CN219603437U - Mixer for glass kiln fuel and fuel supply system - Google Patents

Abstract

The utility model discloses a mixer for glass kiln fuel and a fuel supply system, and belongs to the technical field of glass production. The mixer is arranged between the fuel input pipeline and the fuel spray gun and comprises a horizontally placed outer barrel, wherein two opposite sides of the outer barrel are respectively provided with a feeding end and a discharging end, the feeding end is communicated with a fossil fuel input pipeline and is also communicated with a hydrogen input pipeline and a high-pressure gas input pipeline, and the discharging end of the mixer is communicated with an inlet of the fuel spray gun; the outer cylinder is internally provided with a plurality of mixing paddles for uniformly mixing hydrogen, fossil fuel and high-pressure gas, and the mixing paddles are not overlapped with each other. The mixer can ensure that hydrogen and fossil fuels in various forms are uniformly mixed, so that flame for burning the hydrogen and flame for burning the fossil fuels are not layered, the mixer is suitable for being used in glass melting furnaces, and the carbon dioxide emission is reduced.

Description

Mixer for glass kiln fuel and fuel supply system

Technical Field

The utility model relates to the technical field of glass production, in particular to a mixer for glass kiln fuel and a fuel supply system.

Background

The use of fossil fuels in glass production produces carbon dioxide emissions, with the melting step being one of the most carbon dioxide emitting processes. The prior melting process is a process of melting glass batch materials into glass batch materials by heat generated by fuel combustion in a glass melting furnace, the main mode of melting the glass batch materials is to arrange a plurality of fuel spray guns at intervals on the side wall or the top of the glass melting furnace, the fuel spray guns arranged on the side wall are commonly called side burning spray guns (the side burning spray guns are arranged between the position of the side wall and the two side burning spray guns and are used for spraying combustion improver in small furnace level), the fuel spray guns arranged on the top (such as a big arch) are commonly called top burning spray guns, the fuel is sprayed into the glass melting furnace through the spray guns, the combustion reaction occurs when the fuel is in contact with combustion improver (air or oxygen) sprayed by the small furnace to generate heat, and the generated heat heats and melts the glass batch materials in the glass melting furnace and keeps for a period of time at a certain temperature to form clear and uniform glass batch materials.

Currently, three main types of fuels are used in glass melting processes, one type being gaseous, such as natural gas, coal gas (coal gas is formed by CO, H ₂ Mixed gas composed of methane, etc.), etc.; one type is liquid, such as atomized heavy oil, coal tar, etc.; one type is solid, such as micronized petroleum coke powder, etc. The fuel belongs to the traditional fossil fuel, the main chemical composition is two or three elements in C, H, O, the content of C is the highest, and the main product after the fuel is combusted is CO ₂ 、H ₂ O, etc. so that a large amount of greenhouse gas CO is discharged in the glass production process ₂ . To reduce CO ₂ At present, the method generally adopts the method of improving the combustion efficiency (such as increasing the consumption of the combustion improver or adopting oxygen to replace air as the combustion improver, etc.), or adopts the method of improving the flue gas treatment efficiency (such as end absorption and CO sealing ₂ Etc.), but none of these methods can fundamentally solve CO ₂ The problem of large production amount is solved.

The green fuel, such as hydrogen, is a green clean energy source with high heat value, and can replace the traditional fossil fuel to reduce CO ₂ The amount of production. Replacing fossil fuels with hydrogen is one of the most rapid, effective, and fundamental ways to reduce carbon dioxide emissions. However, the chemical nature of hydrogen is active, the flame generated by combustion is short, the combustion is rapid, local high temperature is easy to occur, the existing fossil fuel is easily burnt out of the kiln and the spray gun system by simply and completely replacing the existing fossil fuel with hydrogen in the fuel supply system of the existing glass kiln, and a large amount of NO is also generated at the local high temperature _x And increasing the load of the subsequent tail gas treatment. When the hydrogen is used for partially replacing fossil fuel, the hydrogen and the fossil fuel are directly mixed and then introduced into the existing spray gun system, and the hydrogen and the fossil fuel cannot be uniformly mixed due to different properties or parameters such as density, state and pressure of the hydrogen and the fossil fuel, so that flame layering is caused, the coverage area of the flame is reduced, and the temperature distribution of the flame is unevenEven, and then reduce its radiation heat transfer effect, also can influence the quality of glass feed liquid.

Disclosure of Invention

The utility model aims at solving the technical defects in the prior art and provides a mixer for glass kiln fuel and a fuel supply system, wherein the mixer can uniformly mix hydrogen with fossil fuel in all states.

The utility model provides a mixer for glass kiln fuel, which is arranged between a fuel input pipeline and a fuel spray gun, and comprises a horizontally placed outer barrel, wherein a feed end and a discharge end are respectively arranged at two opposite sides of the outer barrel, the feed end is communicated with a fossil fuel input pipeline and also communicated with a hydrogen input pipeline and a high-pressure gas input pipeline, and the discharge end of the mixer is communicated with an inlet of the fuel spray gun; a plurality of mixing paddles for uniformly mixing the hydrogen, the fossil fuel and the high-pressure gas are arranged in the outer cylinder, and the mixing paddles are not overlapped with each other; the fossil fuel input pipeline, the hydrogen input pipeline and the high-pressure gas input pipeline are positioned in front of the mixing paddle.

In the mixer for the glass kiln fuel, the outer cylinder is in a cylindrical shape or an elliptic cylindrical shape, the fossil fuel input pipeline is coaxial with the outer cylinder, the hydrogen input pipeline is coaxially sleeved in the fossil fuel input pipeline, and the high-pressure gas input pipeline and the fossil fuel input pipeline are positioned at the same horizontal position and symmetrically distributed on two sides of the fossil fuel input pipeline.

Or the outer cylinder is cylindrical or elliptic cylindrical, the fossil fuel input pipeline is coaxial with the outer cylinder, and the hydrogen input pipeline and the high-pressure gas input pipeline are positioned at the same horizontal position with the fossil fuel input pipeline and are arranged outside the fossil fuel input pipeline at intervals. The fossil fuel input pipelines are positioned on the central axis of the outer cylinder, the number of the hydrogen input pipelines is two, the hydrogen input pipelines are symmetrically distributed on two sides of the fossil fuel input pipelines, a high-pressure gas channel is arranged on the outer side of each hydrogen input pipeline, and the two high-pressure gas channels are symmetrically distributed on two sides of the fossil fuel input pipeline.

In the mixer for the glass kiln spray gun, a plurality of mixing paddles are distributed into one layer or a plurality of layers along the axial direction of the outer barrel, are distributed in a staggered manner along the inner wall of the outer barrel, one end of each mixing paddle is fixed on the inner wall of the outer barrel, the other end of each mixing paddle extends towards the central shaft of the outer barrel, and each mixing paddle inclines towards the discharge end and forms an included angle of not more than 90 degrees with the inner wall of the outer barrel. Wherein:

the mixing paddles are of a planar reticular structure, reticular pores are 5-20mm, the included angle between the mixing paddles and the inner wall of the outer cylinder is 45-80 degrees, and the projection length of the mixing paddles on the radial section of the outer cylinder is not smaller than the radius of the outer cylinder. The mixing paddles are arranged in 5-10 layers in the outer cylinder, and each layer is provided with 3 layers.

Or the mixing paddles are of a planar reticular structure, reticular pores are 22-40mm, the included angle between the mixing paddles and the inner wall of the outer cylinder is 60-90 degrees, and the projection length of the mixing paddles on the radial section of the outer cylinder is smaller than the radius of the outer cylinder; the mixing paddles are arranged in 2-5 layers in the outer cylinder, and each layer is provided with 3 layers.

Or the mixing paddles are of a three-dimensional cambered surface plate-shaped structure, the thickness of the mixing paddles is 10-25cm, only one layer of mixing paddles is arranged in the outer cylinder, the mixing paddles are uniformly distributed along the circumference of the outer cylinder, the inclination directions and the angles are the same, and the projection length of the radial section of the outer cylinder is 1/5-1/4 of the diameter of the outer cylinder.

The utility model also provides a fuel supply system of the glass kiln, which comprises a fuel input pipeline and a fuel spray gun, and further comprises the mixer for the glass kiln fuel, wherein the mixer for the glass kiln fuel is arranged between the fuel input pipeline and the fuel spray gun, the fossil fuel input pipeline is communicated with the feeding end of the mixer, and the fuel spray gun is communicated with the discharging end of the mixer.

The utility model adds a mixer in the existing glass melting furnace, the mixer is arranged between the fuel input pipeline and the fuel spray gun, namely: the feed end of the mixer is communicated with each fuel input pipeline, the discharge end of the mixer is communicated with a fuel spray gun arranged on the side wall or the top of the glass melting furnace, and meanwhile, a hydrogen input pipeline and a high-pressure gas input pipeline are additionally arranged at the feed end of the mixer. The fuel mixer is suitable for fuels with different forms, is provided with the mixing paddles in various forms, can ensure that hydrogen and fossil fuels in various states are uniformly mixed, can prevent flame of hydrogen combustion from layering with flame of fossil fuel combustion when mixed gas introduced into the fuel spray gun from the discharge end of the mixer is combusted, has uniform flame temperature and maximized flame coverage area, ensures good flame heat transfer effect, can accelerate heat transfer of glass feed liquid, ensures stable glass feed liquid temperature and quality, and reduces carbon dioxide emission.

Drawings

FIG. 1 is a schematic cross-sectional top view showing the structure of a fuel supply system in accordance with embodiment 1;

FIG. 2 is a schematic side view in longitudinal section of the mixer structure of example 1;

FIG. 3 is a schematic cross-sectional view showing a top view of the structure of the fuel supply system in embodiment 2;

FIG. 4 is a schematic side view in longitudinal section of the mixer structure of example 2;

FIG. 5 is a schematic top view in transverse cross section showing the structure of a fuel supply system in embodiment 3;

FIG. 6 is a schematic side view in longitudinal section of the mixer structure of example 3;

in the figure: 1-a fossil fuel input pipeline; 2-hydrogen input pipeline; 3-a high pressure gas input conduit; 4-an outer cylinder; 5-mixing paddles; 6-mixer.

Detailed Description

The combustion lances of existing glass kilns typically include side-firing lances (typically positioned at the same level as the small furnace) inside the breast wall and sometimes top-firing lances inside the crown, into which conventional fossil fuels (e.g., gaseous methane CH ₄ Or liquid coal tar or solid petroleum coke powder), the fuel meets combustion improver (air and/or oxygen) introduced by the small furnace at the muzzle to generate flame by combustion reaction, and the glass batch is melted into glass liquid. After the running condition of the current mainstream glass kiln and the combustion mode of the spray gun system are deeply explored, the fuel supply system of the current glass kiln is modified and optimized: a hydrogen input pipeline is additionally arranged, the traditional fossil fuel is partially replaced by green clean fuel, and a high-pressure gas input pipeline is additionally arranged and used for mixing the hydrogen and the fossil fuelThe even mixer adjusts various parameters in the fuel feeding process, such as the types and the pressure of substances fed into various input pipelines, the setting mode of various input pipelines, the internal structure of the mixer and the like, and finally realizes the effective reduction of CO in the fuel combustion process ₂ The generation amount of the glass material liquid can ensure that hydrogen and fossil fuels in all states can be uniformly mixed, flame generated by burning mixed gas of the hydrogen and the fossil fuels is not layered, and the flame burning temperature is uniform, so that the stability of the glass material liquid quality is ensured. Meanwhile, the flame temperature is uniform, so that local high temperature is not generated, and a large amount of NO is not generated locally _x The load of the subsequent tail gas treatment is not increased. In addition, the combustion products H generated by the combustion of hydrogen ₂ The O is also uniformly distributed, so that Si-OH is generated on the surface of the glass feed liquid, the viscosity of the surface of the glass feed liquid is reduced, and the melting and clarification of the glass feed liquid are further promoted. The uniform mixing of the fuel can also lead the coverage area of the flame to be large, lead the heat transfer effect of the flame to be good, accelerate the heat transfer of the glass feed liquid and save the fuel.

The fuel mixer 6 (shown in fig. 1 for example) provided by the utility model is arranged between a fuel input pipeline (positioned on the left side of fig. 1) and a fuel spray gun (positioned on the right side of fig. 1, not shown in the drawings), the feed end of the mixer 6 is communicated with the outlet of each fuel input pipeline, and the discharge end of the mixer is communicated with the inlet of the fuel spray gun. The mixer 6 comprises a horizontally placed cylindrical or elliptic cylindrical outer cylinder 4 (the radial section is circular or elliptic), and one end (the left end is shown in fig. 1) of the outer cylinder 4 is provided with a hydrogen input pipeline 2, a fossil fuel input pipeline 1 and a high-pressure gas input pipeline 3 as feed ends; the hydrogen input pipeline 2 can be coaxially sleeved in the fossil fuel input pipeline 1 (shown in fig. 3 and 5), and can also be independently arranged outside the fossil fuel input pipeline 1 (shown in fig. 1); when the hydrogen gas input pipeline 2 is arranged outside the fossil fuel input pipeline 1, the high-pressure gas input pipeline 3, the hydrogen gas input pipeline 2 and the fossil fuel input pipeline 1 are distributed in sequence from outside to inside along the radial direction of the outer cylinder 4 (taking the outer wall of the outer cylinder as the outer side and taking the axis of the outer cylinder as the inner side). In general, when the fossil fuel input pipe 1 is coaxial with the outer cylinder 4 and the high-pressure gas input pipe 3 and the hydrogen input pipe 2 are provided in plural, the fossil fuel input pipe 1 is arranged at one end of the inner part of the outer cylinder 4 in an axisymmetric manner. The purpose of the high pressure gas input pipe 3 is to form a high pressure jet between the fossil fuel and the hydrogen, so that the vortex flow in the mixing process of the fossil fuel and the hydrogen is increased to accelerate the mixing speed and the mixing uniformity. The hydrogen and the fossil fuel are mixed in the outer tub 4 and then discharged at the other end (discharge end, which is shown as right end in fig. 1) of the mixer 6, and the discharge end of the mixer 6 communicates with the fuel injection lance to introduce the mixed gas of the hydrogen and the fossil fuel into the fuel injection lance. In order to uniformly mix the hydrogen and the fossil fuel, a plurality of mixing paddles 5 (see fig. 1-6) are arranged in an outer barrel 4 of the mixer 6, the plurality of mixing paddles 5 can be distributed into one or more layers along the axial direction of the outer barrel 4, and outlets of the fossil fuel input pipeline 1, the hydrogen input pipeline 2 and the high-pressure gas input pipeline 3 are positioned in front of the first layer of mixing paddles 5; the mixing paddles 5 may be alternately arranged along the inner wall of the outer cylinder 4 at intervals, for example, spirally and alternately arranged along the radial direction and the axial direction of the outer cylinder 4. One end of each mixing paddle 5 is provided on the inner wall of the outer tube 4, the other end extends toward the axis of the outer tube 4, and the mixing paddles 5 do not overlap each other. The mixing paddles 5 are a metal mesh structure made of stainless steel wires or a plate-like structure made of low carbon steel or stainless steel.

The present utility model will be described more specifically with reference to the following examples, which are not intended to limit the present utility model in any way.

Example 1

The fuel supply system of this embodiment has the following modifications, see fig. 1 and 2: introducing gaseous fossil fuel such as natural gas into the fossil fuel input pipeline 1 in the mixer 6, wherein the pressure is 0.03-0.07MPa; introducing hydrogen accounting for 5-40% of the volume of the gaseous fossil fuel into the hydrogen input pipeline 2, wherein the pressure is 0.01-0.03MPa; high-pressure natural gas (or high-pressure methane) is introduced into the high-pressure gas input pipeline 3, and the pressure is 0.25-0.6MPa. The fossil fuel input pipeline 1 is arranged on the axis of the outer barrel 4, the hydrogen input pipeline 2 is arranged outside the fossil fuel input pipeline 1 and is arranged with the fossil fuel input pipeline 1 as axisymmetric, the high-pressure gas input pipeline 3 is arranged outside the hydrogen input pipeline 2 (closer to the outer barrel 4) and is also arranged with the fossil fuel input pipeline 1 as axisymmetric, namely, the hydrogen input pipeline 2 and the high-pressure gas input pipeline 3 are sequentially and symmetrically distributed from inside to outside on two sides of the fossil fuel input pipeline 1. The hydrogen input pipeline 2 and the high-pressure gas input pipeline 3 are positioned at the same horizontal position with the fossil fuel input pipeline 1. The mixing paddles 5 in the mixer 6 are metal nets woven by stainless steel wires, the holes of the metal nets are 5-20mm, and the diameters of the metal wires are 3-6mm; each mixing paddle 5 is a planar metal net, one end of each mixing paddle is welded on the inner wall of the outer barrel 4, the other end of each mixing paddle extends towards the central axis of the outer barrel 4 and inclines towards the discharge end of the outer barrel (namely, the fuel flow direction is from left to right in fig. 1), and the included angle between each mixing paddle 5 and the inner wall of the outer barrel 4 is 45-80 degrees (namely, the included angle between each mixing paddle 5 and the fuel flow direction is 100-135 degrees). The mixing paddles 5 are arranged in 5-10 layers (see fig. 1) along the axis of the outer cylinder in the outer cylinder 4, 3 layers (see fig. 2) are arranged on each layer, the mixing paddles 5 on the same layer are uniformly distributed along the circumference of the outer cylinder 4, and the inclination directions and the angles of the mixing paddles on the same position of each layer are kept the same. Referring to fig. 2, the mixing paddles 5 of the same layer are inserted into the outer barrel 4 to a length such that the mixing paddles 5 extend at least to the axial position of the outer barrel 4 and even beyond the axis of the outer barrel 4, i.e., the projection length of the mixing paddles 5 on the radial cross section of the outer barrel 4 is not smaller than the radius of the outer barrel 4, so that the projections of the mixing paddles 5 of the same layer on the radial cross section of the outer barrel 4 overlap (due to the inclination of the mixing paddles 5), but the mixing paddles 5 of each layer do not overlap each other.

The method of fuel mixing using the mixer of the present embodiment: natural gas is sequentially introduced into the fossil fuel input pipeline 1 according to the pressure, hydrogen is introduced into the hydrogen input pipeline 2, and high-pressure natural gas is introduced into the high-pressure gas input pipeline 3. The three materials are mixed to form mixed gas in the process of flowing from the feeding end to the discharging end of the mixer 6, and the mixed gas finally reaches the combustion spray gun of the glass melting furnace to be sprayed out for combustion reaction; in the flowing process, the three materials are uniformly mixed under the action of the mixing paddle 5 in the mixer 6, and the pressure of the mixed gas of the three materials is regulated to be uniform to 0.035-0.065MPa. The high-pressure natural gas is introduced to form high-pressure jet flow in the mixed fuel of natural gas and hydrogen so as to increase the vortex flow of the mixed fuel and speed up the mixing speed and the mixing uniformity, thereby avoiding the forward movement process and the burning of the mixed fuelDelamination during firing. The addition of hydrogen can reduce CO in the combustion process ₂ The amount of production.

Application of the present embodiment: taking a 600t/d glass production line as an example, the common soda-lime-silica glass batch is melted to 1580 ℃ by using the mixing method of the embodiment, wherein the pressure of natural gas in the fossil fuel input pipeline 1 is 0.05MPa; the hydrogen input pipeline 2 is filled with hydrogen with the volume of 20% of the volume of the gaseous fossil fuel and the pressure of 0.02MPa; the pressure of the high-pressure natural gas in the high-pressure gas input pipeline 3 is 0.4MPa. The mixing paddles 5 are metal nets woven by stainless steel wires, the holes of the metal nets are 10mm, and the diameters of the wires are 5mm; the mixing paddles 5 have an angle of 60 ° with the inner wall of the outer barrel 4 (i.e., the mixing paddles 5 have an angle of 120 ° with the direction of fuel flow). The mixing paddles 5 are arranged in 7 layers (as shown in fig. 1) within the outer barrel 4. The length of the mixing paddles 5 of the same layer inserted into the outer cylinder 4 (the mixing paddles 5 are inclined, and the length refers to the projection length thereof) is 2/3 of the diameter of the outer cylinder 4. The pressure of the mixed fuel at the discharge end of the mixer 6 was 0.05MPa.

The application implements data: annual CO ₂ The discharge amount was 9.5 ten thousand tons (260.3 tons/day), and the annual hydrogen consumption amount was 876 ten thousand Nm ³ (2400Nm ³ Per year natural gas consumption is 3504 ten thousand Nm ³ (96000Nm ³ And/d), the temperature difference of the glass liquid cross section in the glass kiln is less than 10 ℃, and the transverse temperature difference of the flame space is less than 15 ℃. Whereas the mixing method of the prior glass kiln (taking natural gas as fuel, and not using the mixing method and the mixer of the utility model) is used for CO every year ₂ The discharge amount is 14 ten thousand tons (1 ten thousand tons of CO) ₂ The discharge amount is equivalent to 1000 ten thousand Nm ³ The temperature difference of the glass liquid cross section in the glass kiln is less than 20-30 ℃ and the transverse temperature difference of the flame space is less than 20 ℃.

Comparative example 1-1: the common soda-lime-silica glass batch was melted to 1580 ℃ by the parameters of the mixer and the mixing method of example 1, except that the angle between the mixing paddles 5 and the inner wall of the outer barrel 4 was changed to 30 ° (i.e., the angle between the mixing paddles 5 and the fuel flow direction was 150 °), and the other conditions were unchanged, and the CO for producing 600t glass per day was converted ₂ The discharge amount was 265 tons/day, and the hydrogen consumption amount was 25800Nm ³ /d, glassThe temperature difference of the glass liquid cross section in the glass kiln is 10-15 ℃, and the transverse temperature difference of the flame space is less than 18 ℃.

Comparative examples 1-2: the common soda-lime-silica glass batch was melted to 1580 ℃ by the parameters of the mixer and the mixing method of example 1, except that the angle between the mixing paddles 5 and the inner wall of the outer barrel 4 was changed to 100 ° (i.e., the angle between the mixing paddles 5 and the fuel flow direction was 80 °), and the other conditions were unchanged, and the CO for producing 600t glass per day was converted ₂ The discharge amount was 281 tons/day, and the hydrogen consumption amount was 26300Nm ³ And/d, the temperature difference of the glass liquid cross section in the glass kiln is 12-17 ℃, and the transverse temperature difference of the flame space is less than 20 ℃.

Comparative examples 1-3: the common soda-lime-silica glass batch was melted to 1580℃by the parameters of the mixer and the mixing method of example 1, except that the mixed fuel pressure at the discharge end of the mixer 6 was adjusted to 0.02MPa, and the other conditions were unchanged, and the CO for producing 600t glass per day was converted ₂ The discharge amount was 277 tons/day, and the hydrogen consumption amount was 22200Nm ³ And/d, the temperature difference of the glass liquid cross section in the glass kiln is 13-15 ℃, and the transverse temperature difference of the flame space is less than 19 ℃.

Comparative examples 1 to 4: the common soda-lime-silica glass batch was melted to 1580℃by the parameters of the mixer and the mixing method of example 1, except that the mixed fuel pressure at the discharge end of the mixer 6 was adjusted to 0.08MPa, and the other conditions were unchanged, and the CO for producing 600t glass per day was converted ₂ The discharge amount was 272 tons/day, and the hydrogen consumption amount was 27700Nm ³ And/d, the temperature difference of the glass liquid cross section in the glass kiln is 15-22 ℃, and the transverse temperature difference of the flame space is less than 25 ℃.

Example 2

The fuel supply system provided in this embodiment has the following modifications, see fig. 3 and 4: the fossil fuel input pipeline 1 in the mixer 6 is filled with liquid fossil fuel such as atomized heavy oil or coal tar, for example, the heavy oil with the pressure of 0.3-0.6MPa; the hydrogen input pipeline 2 is filled with hydrogen with the volume of 5-40% of the liquefied fossil fuel and the pressure of 0.1-0.3MPa; high-pressure air is introduced into the high-pressure gas input pipeline 3, and the pressure is 0.5-0.7MPa. The fossil fuel input pipeline 1 is arranged on the axis of the outer barrel 4, the hydrogen input pipeline 2 is coaxially sleeved in the fossil fuel input pipeline 1, and the high-pressure gas input pipeline 3 and the fossil fuel input pipeline 1 are positioned at the same horizontal position and symmetrically arranged on two sides of the fossil fuel input pipeline 1 (see fig. 3). The mixing paddles 5 in the mixer 6 are metal nets woven by stainless steel wires, the pores of the metal nets are 22-40mm, and the diameters of the metal wires are 5-10mm; each mixing paddle 5 is a planar metal net, one end of each mixing paddle is welded on the inner wall of the outer cylinder 4, and the other end extends towards the central axis of the outer cylinder 4 and inclines towards the discharge end (along the fuel flow direction, the angle between the mixing paddles 5 and the inner wall of the outer cylinder 4 is 60-90 degrees (namely, the angle between the mixing paddles 5 and the fuel flow direction is 90-120 degrees). The mixing paddles 5 are arranged in the outer cylinder 4 in 2-5 layers, each layer is provided with 3 layers, the mixing paddles 5 on the same layer are uniformly distributed along the circumference of the outer cylinder 4, and the inclination directions and angles of the mixing paddles on the same position of each layer are kept the same. The mixing paddles 5 of the same layer are inserted into the outer cylinder 4 to a length of 1/3-2/3 of the radius of the outer cylinder 4, and the mixing paddles 5 extend in the outer cylinder 4 to a position not exceeding the axis of the outer cylinder 4, i.e. the projection length of the mixing paddles 5 on the radial section of the outer cylinder 4 is smaller than the radius of the outer cylinder 4, so that the projections of the mixing paddles 5 of the same layer on the radial section of the outer cylinder 4 are not overlapped (see fig. 4). The number of layers of mixing paddles 5 in the mixer of this example is smaller than that of example 1, mainly because the viscosity of liquid fossil fuel is higher than that of gaseous fossil fuel, and the metal mesh is easily blocked. The length of the mixing paddles 5 inserted into the outer cylinder 4 in the mixer of the embodiment is smaller than that of the embodiment 1, and the mixing effect is prevented from being influenced after the mixing paddles 5 are impacted and deformed due to the large heavy oil pressure.

The method of fuel mixing using the mixer of the present embodiment: heavy oil is sequentially introduced into the fossil fuel input pipeline 1 according to the pressure, hydrogen is introduced into the hydrogen input pipeline 2, and high-pressure air is introduced into the high-pressure gas input pipeline 3. The three materials flow from the feeding end to the discharging end of the mixer 6 and finally reach the combustion spray gun of the glass melting furnace to be sprayed out for combustion reaction; in the flowing process, the three materials are uniformly mixed under the action of the mixing paddle 5 in the mixer 6, and the pressure after the three materials are mixed is regulated to be uniform to 0.4-0.5MPa. The high-pressure air can form high-pressure jet flow in the mixed fuel of heavy oil and hydrogen so as to make the mixed fuelThe vortex is increased, the mixing speed and the mixing uniformity are accelerated, and therefore layering of the mixed fuel in the forward movement process and the combustion process is avoided. The addition of hydrogen can reduce CO in the combustion process ₂ The amount of production.

Application of the present embodiment: taking a 600t/d glass production line as an example, the common soda-lime-silica glass batch is melted to 1580 ℃ by using the mixing method of the embodiment, wherein the pressure of heavy oil in the fossil fuel input pipeline 1 is 0.5MPa; the hydrogen input pipeline 2 is filled with hydrogen with the volume of 20% of the volume of the gaseous fossil fuel and the pressure of 0.2MPa; the pressure of the high-pressure air in the high-pressure gas input pipeline 3 is 0.6MPa. The mixing paddles 5 are metal nets woven by stainless steel wires, the holes of the metal nets are 30mm, and the diameters of the wires are 7mm; the mixing paddles 5 are at an angle of 75 ° to the inner wall of the outer barrel 4 (i.e., the mixing paddles 5 are at an angle of 105 ° to the direction of fuel flow). The mixing paddles 5 are arranged in 3 layers (as shown in fig. 1) within the outer barrel 4. The length of the mixing paddles 5 of the same layer inserted into the outer barrel 4 is 2/3 of the radius of the outer barrel 4. The pressure of the mixed fuel at the discharge end of the mixer 6 was 0.45MPa.

The application implements data: annual CO ₂ The discharge amount was 9.8 ten thousand tons (268.5 tons/day), and the annual hydrogen consumption amount was 876 ten thousand Nm ³ (24000Nm ³ Per d), the annual heavy oil consumption is 52560t (144 t/d), the temperature difference of the glass liquid cross section in the glass kiln is less than 12 ℃ and the transverse temperature difference of the flame space is less than 30 ℃. The mixing method of the prior glass kiln (taking heavy oil as fuel, and not using the mixing method and the mixer) is used for CO per year ₂ The discharge amount is 14 ten thousand tons (1 ten thousand tons of CO) ₂ The discharge amount is equivalent to 5363 tons of heavy oil consumption, the temperature difference of the glass liquid cross section in the glass kiln is 15-22 ℃, and the transverse temperature difference of the flame space is less than 22 ℃.

Comparative example 2-1: the common soda-lime-silica glass batch was melted to 1580 ℃ by the parameters of the mixer and the mixing method of example 2, except that the angle between the mixing paddles 5 and the inner wall of the outer barrel 4 was changed to 45 ° (i.e., the angle between the mixing paddles 5 and the fuel flow direction was 135 °), and the other conditions were unchanged, and the CO for 600t glass per day was converted ₂ The discharge amount was 269 ton/day, and the hydrogen consumption amount was 25900Nm ³ And/d, the temperature difference of the glass liquid cross section in the glass kiln is 15-21 ℃, and the transverse temperature difference of the flame space is less than 21 ℃.

Comparative example 2-2: the common soda-lime-silica glass batch was melted to 1580 ℃ by the parameters of the mixer and the mixing method of example 2, except that the angle between the mixing paddles 5 and the inner wall of the outer barrel 4 was changed to 105 ° (i.e., the angle between the mixing paddles 5 and the fuel flow direction was 75 °), and the other conditions were unchanged, and the CO for producing 600t glass per day was converted ₂ The discharge amount was 285 tons/day, and the hydrogen consumption amount was 26300Nm ³ And/d, the temperature difference of the glass liquid cross section in the glass kiln is 14-20 ℃, and the transverse temperature difference of the flame space is less than 23 ℃.

Comparative examples 2-3: the common soda-lime-silica glass batch was melted to 1580℃by the parameters of the mixer and the mixing method of example 2, except that the mixed fuel pressure at the discharge end of the mixer 6 was adjusted to 0.3MPa, and the other conditions were unchanged, and converted to CO for 600t glass per day ₂ The discharge amount was 275 tons/day, and the hydrogen consumption amount was 22300Nm ³ And/d, the temperature difference of the glass liquid cross section in the glass kiln is 14-17 ℃, and the transverse temperature difference of the flame space is less than 20 ℃.

Comparative examples 2 to 4: the common soda-lime-silica glass batch was melted to 1580℃by the parameters of the mixer and the mixing method of example 1, except that the mixed fuel pressure at the discharge end of the mixer 6 was adjusted to 0.6MPa, and the other conditions were unchanged, and the CO for producing 600t glass per day was converted ₂ The discharge amount was 273 tons/day, and the hydrogen consumption amount was 28900Nm ³ And/d, the temperature difference of the glass liquid cross section in the glass kiln is 13-19 ℃, and the transverse temperature difference of the flame space is less than 20 ℃.

Example 3

The fuel supply system provided in this embodiment has the following modifications, see fig. 5 and 6: solid fossil fuel, such as micronized petroleum coke powder (300 meshes), is introduced into the fossil fuel input pipeline 1 in the mixer 6, and the pressure is 0.4-0.55MPa; the hydrogen input pipeline 2 is filled with hydrogen with the volume of 5-40% of the solid fossil fuel and the pressure of 0.01-0.03MPa; high-pressure air is introduced into the high-pressure gas input pipeline 3, and the pressure is 0.5-0.7MPa. The fossil fuel input pipeline 1 is arranged on the axis of the outer barrel 4, the hydrogen input pipeline 2 is coaxially sleeved in the fossil fuel input pipeline 1, and the high-pressure gas input pipeline 3 and the fossil fuel input pipeline 1 are positioned at the same horizontal position and symmetrically arranged on two sides of the fossil fuel input pipeline 1 (see fig. 5). The mixing paddles 5 in the mixer 6 are plates made of low carbon steel or stainless steel; referring to fig. 6, each mixing paddle 5 is a solid arc panel (e.g., fan blade-like) having a thickness of 10-25cm, one end side is welded to the inner wall of the outer tub 4, the other end extends toward the center axis of the outer tub 4 and its arc surface is inclined in the fuel flow direction (shown from left to right in fig. 5). The mixing paddles 5 are only arranged in the outer barrel 4 in one layer, the mixing paddles 5 are uniformly distributed along the circumference of the outer barrel 4, and the radial section of the outer barrel 4 is in the form of fan blades like an electric fan or impeller blades in an aircraft engine; the length of the mixing paddles 5 extending into the outer barrel 4 (the projection length in the radial cross section of the outer barrel) is 1/5-1/4 of the diameter of the outer barrel 4, i.e. the position of the mixing paddles 5 extending within the outer barrel 4 not beyond the axis of the outer barrel 4, such that the projections of the mixing paddles 5 on the radial cross section of the outer barrel 4 do not overlap. In this embodiment, only solid fossil fuel is used, so that even mixing can be realized by providing a layer of mixed slurry 5 in a specific form.

The method of fuel mixing using the mixer of the present embodiment: the micronized petroleum coke powder is sequentially introduced into the fossil fuel input pipeline 1 according to the design conditions, the hydrogen is introduced into the hydrogen input pipeline 2, and the high-pressure air is introduced into the high-pressure gas input pipeline 3. The three materials flow from the feeding end to the discharging end of the mixer 6 and finally reach the combustion spray gun of the glass melting furnace to be sprayed out for combustion reaction; in the flowing process, the three materials are uniformly mixed under the action of the mixing paddle 5 in the mixer 6, and the pressure after the three materials are mixed is regulated to be uniform to 0.43-0.52MPa. The high-pressure air is introduced to form high-pressure jet flow in the mixed fuel of petroleum coke powder and hydrogen, so that the vortex flow of the mixed fuel is increased, the mixing speed and the mixing uniformity are accelerated, and the layering of the mixed fuel in the forward movement process and the combustion process is avoided. The addition of hydrogen can reduce CO in the combustion process ₂ The amount of production.

Application of the present embodiment: taking a 600t/d glass production line as an example, using the mixing method of the embodiment to melt the common soda-lime-silica glass batch to 1580 ℃, wherein the pressure of petroleum coke powder in the fossil fuel input pipeline 1 is 0.50MPa; the hydrogen input pipeline 2 is filled with hydrogen with the volume of 20% of the volume of the gaseous fossil fuel and the pressure of 0.02MPa; the pressure of the high-pressure air in the high-pressure gas input pipeline 3 is 0.6MPa. The thickness of the mixing paddles 5 is 18cm. The length of the mixing paddles 5 inserted into the outer barrel 4 is 1/4 of the diameter of the outer barrel 4. The mixed fuel pressure at the discharge end of the mixer 6 was 0.48MPa.

The application implements data: annual CO ₂ The discharge amount was 11.3 ten thousand tons (309.6 tons/day), and the annual hydrogen consumption amount was 876 ten thousand Nm ³ (2400Nm ³ Per year, the consumption of petroleum coke powder is 55480t (152 t/d), the temperature difference of glass liquid cross section in the glass kiln is 14 ℃, and the transverse temperature difference of flame space is 30-35 ℃. The prior glass kiln production method (taking petroleum coke powder as fuel and not using the mixing method and the mixer) uses CO every year ₂ The discharge amount is 14 ten thousand tons (1 ten thousand tons of CO) ₂ The discharge amount is equivalent to the temperature difference of 17-28 ℃ of the glass liquid cross section in the glass kiln, which is generated by burning 4910 tons of petroleum coke powder, and the transverse temperature difference of flame space is less than 37 ℃.

Comparative example 3-1: the common soda-lime-silica glass batch was melted to 1580℃by the parameters of the mixer and the mixing method of example 3, except that the mixed fuel pressure at the discharge end of the mixer 6 was adjusted to 0.35MPa, and the other conditions were unchanged, and the CO for producing 600t glass per day was converted ₂ The discharge amount was 339 tons/day, and the hydrogen consumption amount was 2400Nm ³ And/d, the temperature difference of the glass liquid cross section in the glass kiln is 16-22 ℃, and the transverse temperature difference of the flame space is 42-47 ℃. The main reason for the variation of the effect of the comparative example is that the flame length is shortened after the pressure is low, the flame coverage area is reduced, the temperature difference is increased, and the emission is increased.

Comparative example 3-2: melting common soda-lime-silica glass batch to 1580deg.C with the fuel parameters of example 3 (petroleum coke powder pressure 0.50MPa; hydrogen gas inlet amount 20% of gaseous fossil fuel volume, pressure 0.02 MPa) without using mixer, feeding all the fuels into glass melting furnace separately, directly feeding into furnace without mixing for combustion, and converting to obtain CO for 600t glass production per day under the same conditions ₂ The discharge amount is 383 tons/dayThe hydrogen consumption was 2400Nm ³ And/d, the temperature difference of the glass liquid cross section in the glass kiln is 23-29 ℃, and the transverse temperature difference of the flame space is less than 50-65 ℃. The comparative example shows that no mixing has combustion stratification, which is disadvantageous for stable combustion.

Comparative examples 3-3: the common soda-lime-silica glass batch was melted to 1580℃using the parameters of the mixer and the mixing method of example 3, except that the mixed fuel pressure at the discharge end of mixer 6 was 0.8MPa, the other conditions were unchanged, and the conversion was carried out to obtain CO for 600t glass per day ₂ The discharge amount was 357 tons/day, and the hydrogen consumption amount was 2400Nm ³ And/d, the temperature difference of the glass liquid cross section in the glass kiln is 15-25 ℃, and the transverse temperature difference of the flame space is 47-53 ℃. The comparative example shows that after the pressure of the mixed fuel is increased, the incompletely combusted fuel can be burnt in opposite side heat accumulation, so that the energy consumption is increased and the kiln structure is burnt.

The foregoing is merely a preferred embodiment of the utility model, and it should be noted that modifications and adaptations to those skilled in the art may be made without departing from the principles of the present utility model, which are intended to be comprehended by the present utility model.

Claims (10)

1. The mixer for the glass kiln fuel is arranged between a fuel input pipeline and a fuel spray gun and is characterized by comprising a horizontally arranged outer barrel, wherein a feeding end and a discharging end are respectively arranged on two opposite sides of the outer barrel, the feeding end is communicated with a fossil fuel input pipeline and is also communicated with a hydrogen input pipeline and a high-pressure gas input pipeline, and the discharging end of the mixer is communicated with an inlet of the fuel spray gun; a plurality of mixing paddles for uniformly mixing the hydrogen, the fossil fuel and the high-pressure gas are arranged in the outer cylinder, and the mixing paddles are not overlapped with each other; the fossil fuel input pipeline, the hydrogen input pipeline and the high-pressure gas input pipeline are positioned in front of the mixing paddle.

2. The mixer for glass kiln fuel according to claim 1, wherein the outer cylinder is in a cylindrical shape or an elliptic cylindrical shape, the fossil fuel input pipeline is coaxial with the outer cylinder, the hydrogen input pipeline is coaxially sleeved in the fossil fuel input pipeline, and the high-pressure gas input pipeline and the fossil fuel input pipeline are positioned at the same horizontal position and are symmetrically distributed on two sides of the fossil fuel input pipeline.

3. The mixer for glass kiln fuel according to claim 1, wherein the outer tub is cylindrical or elliptical cylindrical, the fossil fuel input pipe is coaxial with the outer tub, and the hydrogen input pipe and the high-pressure gas input pipe are at the same horizontal position as the fossil fuel input pipe and are arranged outside the fossil fuel input pipe with a spacing therebetween.

4. The mixer for glass kiln fuel according to claim 3, wherein the fossil fuel input pipelines are located on the central axis of the outer cylinder, the hydrogen input pipelines are two and symmetrically distributed on two sides of the fossil fuel input pipelines, a high-pressure gas channel is arranged on the outer side of each hydrogen input pipeline, and the two high-pressure gas channels are symmetrically distributed on two sides of the fossil fuel input pipeline.

5. The mixer for glass kiln fuel according to any one of claims 1 to 4, wherein a plurality of the mixing paddles are distributed in one or more layers along the axial direction of the outer barrel, are alternately distributed along the inner wall of the outer barrel, one end of each mixing paddle is fixed on the inner wall of the outer barrel, the other end extends toward the central axis of the outer barrel, and the mixing paddles are inclined toward the discharge end and have an included angle of not more than 90 ° with the inner wall of the outer barrel.

6. The mixer for glass kiln fuel according to claim 5, wherein the mixing paddles have a planar net-shaped structure, net-shaped holes are 5-20mm, an included angle between the mixing paddles and the inner wall of the outer cylinder is 45-80 degrees, and the projection length of the mixing paddles on the radial section of the outer cylinder is not smaller than the radius of the outer cylinder.

7. The mixer for glass kiln fuel according to claim 6, wherein the mixing paddles are provided in 5-10 layers in the outer barrel.

8. The mixer for the glass kiln fuel according to claim 5, wherein the mixing paddles are of a planar net-shaped structure, net-shaped holes are 22-40mm, an included angle between the mixing paddles and the inner wall of the outer cylinder is 60-90 degrees, and the projection length of the mixing paddles on the radial section of the outer cylinder is smaller than the radius of the outer cylinder; the mixing paddles are arranged in the outer cylinder for 2-5 layers.

9. The mixer for glass kiln fuel according to claim 5, wherein the mixing paddles are of a three-dimensional cambered surface plate-shaped structure, the thickness of the mixing paddles is 10-25cm, only one layer of mixing paddles is arranged in the outer cylinder, the plurality of mixing paddles are uniformly distributed along the circumference of the outer cylinder and have the same inclination direction and angle, and the projection length of the radial section of the outer cylinder is 1/5-1/4 of the diameter of the outer cylinder.

10. A fuel supply system for a glass kiln, comprising a fuel input pipeline and a fuel spray gun, and further comprising the glass kiln fuel mixer according to any one of claims 1-9, wherein the glass kiln fuel mixer is arranged between the fuel input pipeline and the fuel spray gun, the fossil fuel input pipeline is communicated with a feed end of the mixer, and the fuel spray gun is communicated with a discharge end of the mixer.